Method for processing a sulfur-containing gas and a hydrogenation catalyst used therefor

ABSTRACT

The present invention relates to a method for processing a sulfur-containing gas and a hydrogenation catalyst used therefor. The method comprises introducing the sulfur-containing gas into the tail gas hydrogenation unit of a sulfur recovery device, processing it with the hydrogenation catalyst of the present invention, and absorbing the hydrogenated tail gas with a solvent. The hydrogenation catalyst comprises from 0.5 to 3 wt. % of an active component nickel oxide, from 1 to 4 wt. % of an active component cobalt oxide, from 8 to 20 wt. % of an active component molybdenum oxide or tungsten oxide, from 1 to 5 wt. % of a deoxidation auxiliary agent, from 10 to 40 wt. % of TiO2, the balance being γ-Al2O3, based on the weight of the catalyst.

CROSS REFERENCES TO RELATED APPLICATIONS

This application is a national stage entry of International ApplicationNo.: PCT/CN2011/001283 filed Aug. 4, 2011, which in turn claims priorityto China Patent Application No. 201010269123.7 filed Sep. 1, 2010; eachof which is hereby incorporated by reference herein in its entirety.

TECHNICAL FIELD

The present invention relates to a method for processing asulfur-containing gas, in particular a flue gas regenerated byabsorptive desulfurization of gasoline, and a hydrogenation catalystused therefor.

BACKGROUND

In order to increase the quality of automobile gasoline, SINOPEC makessecondary development on the patent technology of absorptivedesulfurization of gasoline purchased from ConocoPhillips, to producelow-sulfur clean gasoline having a sulfur content of lower than 10 ppm.SINOPEC has established eight sets of the gasoline-absorptivedesulfurization equipment in the first phase, and will build severalsets of the equipments in the second phase. The processing of theregenerated flue gas has become an important part indispensable to theequipment construction.

The adsorbent for absorptive desulfurization of gasoline needs to beregenerated by calcining after saturated by absorption, and theregenerated flue gas contains sulfur dioxide in a higher content. In theoriginal patent, sulfur dioxide is removed by absorption with analkaline solution. However, the processing of waste alkaline solutionwill result in secondary pollution, and waste the sulfur resources atthe same time.

At present, no patent of introducing the flue gas regenerated byabsorptive desulfurization of gasoline into the Claus tail gashydrogenation unit of a sulfur device has been reported yet. This isprimarily because that the regenerated flue gas comprises SO₂ in amaximum volume content of 5.4% and O₂ in a maximum volume content of3.0%, and has a temperature of only 160° C., while the Claus tail gashydrogenation catalyst in the prior art requires the SO₂ volume contentof less than 0.5%, the O₂ volume content of less than 0.05% and atemperature of more than 280° C. Thus the Claus tail gas hydrogenationcatalyst in the prior art cannot satisfy the requirements onhydrogenation of the flue gas regenerated by absorptive desulfurizationof gasoline.

SUMMARY OF THE INVENTION

The present invention solves the aforesaid technical problem byproviding a hydrogenation and deoxidation catalyst special for thesulfur-containing gas, and a method for processing suchsulfur-containing gas. The catalyst of the present application has ahigh hydrogenation activity for sulfur dioxide and a low workingtemperature. In addition, the method for processing thesulfur-containing gas of the present invention can not only recover thesulfur resources, but also avoid the environmental pollution.

In one embodiment, the hydrogenation catalyst for hydrogenation of thesulfur-containing gas of the present invention is characterized incomprising from 0.5 to 3 wt. % of an active component nickel oxide, from1 to 4 wt. % of an active component cobalt oxide, from 8 to 20 wt. % ofan active component molybdenum oxide or tungsten oxide, from 1 to 5 wt.% of a deoxidation auxiliary agent, from 10 to 40 wt. % of TiO₂, thebalance being γ-Al₂O₃, based on the weight of the catalyst.

In another embodiment, the deoxidation auxiliary gent is one or moreselected from the group consisting of ferrous sulfate, ferric nitrate,ferric sulfate, palladium chloride and platinum chloride, preferablyferrous sulfate.

In another embodiment, the catalyst comprises from 1.0 to 1.5 wt. % ofan active component nickel oxide, from 2.0 to 3.0 wt. % of an activecomponent cobalt oxide, from 12 to 15 wt. % of an active componentmolybdenum oxide or tungsten oxide, from 2 to 4 wt. % of a deoxidationauxiliary agent, from 20 to 30 wt. % of TiO₂, the balance being γ-Al₂O₃,based on the weight of the catalyst. In another embodiment, thesulfur-containing gas comprises from 0 to 6 vol. % of sulfur dioxide andfrom 0 to 3 vol. % of oxygen, and has a temperature of preferably from100 to 200° C.

In another embodiment, the catalyst is produced by usingtitanium-aluminum compound dry colloid as the main raw material,bar-extruding, drying, calcining to prepare a support; said supportbeing impregnated with a deoxidation auxiliary agent, dried, calcined toproduce a semi-finished product; said semi-finished product beingimpregnated with an impregnation solution of the active component,further dried and calcined.

Said titanium-aluminum compound dry colloid is prepared by placing asodium metalluminate solution being diluted to 5-60 g of Al₂O₃/L in acolloidization tank, controlling the colloid-forming temperature to be0-30° C., feeding CO₂ having a volume concentration of 3-40% forneutralization, pulping metatitanic acid, slowly adding metatitanic acidslurry for a period of time which is controlled to be 10-20 min when CO₂begins to be fed, so as to make the weight content of titania achieve30-60% in the dry colloid, controlling the pH value of the glue solutionto be 10-12, stopping the colloidization, filtering, washing, drying andpulverizing to 180 meshes, to produce a titanium-aluminum compound drycolloid.

The titanium-aluminum compound dry colloid has a pore volume of greaterthan 0.6 ml/g, a specific surface area of greater than 250 m²/g, asodium weight content of less than 0.1%, and a SO₄ ²⁻ weight content ofless than 0.2%. Preferably, the titanium-aluminum compound dry colloidhas a pore volume of from 0.60 to 0.90 mL/g, a specific surface area offrom 270 to 380 m²/g, a sodium weight content of less than 0.1%, and aSO₄ ²⁻ weight content of less than 0.2%.

The active component is a ternary component consisting of one selectedfrom the Group VIB elements and two selected from the Group VIII metalelements.

The catalyst has the advantages of high COS and CS₂ hydrolysis activityand SO₂ hydrogenation activity at lower reaction temperature, removingoxygen from the sulfur-containing gas by adding a deoxidation auxiliaryagent, using as the active component the ternary metal of Groups VIB andVIII so as to increase the SO₂ hydrogenation activity.

In another embodiment, the catalyst of the present invention is preparedby the following method:

-   -   mixing and kneading a titanium-aluminum compound dry colloid        having a pore volume of more than 0.6 mL/g, a specific surface        area of greater than 250 m²/g, a sodium content of less than        0.1% (m/m), and a SO₄ ²⁻ content of less than 0.2% (m/m), a        pore-expanding agent and a binder, bar-extruding, drying,        calcining to produce a support;

The support is impregnated with the deoxidation auxiliary agent, dried,calcined to produce a semi-finished product;

The semi-finished product is impregnated with the active componentimpregnation solution, further dried, calcined to produce alow-temperature, oxytolerant hydrogenation catalyst having a highactivity for the sulfur-containing gas.

The pore-expanding agent is selected from the group consisting ofpolyvinyl alcohol, polyacrylamides, sesbania powder, citric acid, starchand the like, preferably sesbania powder.

The binder is selected from the group consisting of water, acetic acid,citric acid, oxalic acid and nitric acid, preferably citric acid.

The support is calcined at a temperature of from 500 to 600° C.,preferably 550° C.

The support has an appearance preferably clover-type or four-leafclover-type.

The support has a pore volume of greater than 0.4 mL/g, preferablygreater than 0.45 mL/g, and a specific surface area of more than 280m²/g, preferably more than 300 m²/g.

The deoxidation auxiliary gent is one or more selected from the groupconsisting of ferrous sulfate, ferric nitrate, ferric sulfate, palladiumchloride and platinum chloride, preferably ferrous sulfate.

The semi-finished product is calcined at a temperature of from 350 to450° C., preferably 400° C.

The active component is a ternary component selected from Group VIBelements and/or Group VIII metal elements, and the amount of Group VIBmetal oxides is from 8 to 20% (m/m), preferably from 12% to 15% (m/m),and the amount of Group VIII metal oxides is from 1.5 to 7% (m/m),preferably from 2.5% to 3.5% (m/m), based on the weight of the catalyst.The deoxidation auxiliary agent is in an amount of from 1 to 5%.

The Group VIB metal element is molybdenum or tungsten, preferablymolybdenum, and the precursor is molybdenum oxide; the Group VIII metalelement is cobalt and nickel, and the precursor is nickel carbonate andbasic cobalt carbonate. Since no metal nitrate is used during thepreparation, no NOx is produced during the calcining process, so thatthe preparation is clean and environment-friendly.

The catalyst is calcined at a temperature of from 200 to 500° C.,preferably 400° C.

The preparation process of the present invention is more specificallystated as follows.

1. Preparation of the Support

A titanium-aluminum compound dry colloid having a pore volume of morethan 0.6 mL/g, a specific surface area of greater than 250 m²/g, asodium content of less than 0.1%, and a SO₄ ²⁻ content of less than0.2%, a binder (e.g. water, nitric acid, acetic acid, oxalic acid andcitric acid), a pore-expanding agent (e.g. polyvinyl alcohol,polyacrylamides, sesbania powder, citric acid, starch and the like) areadded into a kneader. The mixture was kneaded, molded by extrusion withφ3 mm clover-type pore plate (or in other shapes), oven-dried at110-150° C. for 2-4 h, calcined at 500-600° C. for 2-5 h to produce asupport comprising from 10 to 40% (m/m), preferably from 20 to 30% (m/m)of TiO₂, and from 40 to 90% (m/m), preferably from 65 to 75% (m/m) ofAl₂O₃.

N₂ absorption process is used to determine the specific surface area andpore volume of the prepared support.

2. Preparation of the Semi-Finished Product

A stabilizer (citric acid, acetic acid, hydrochloric acid or sulfurousacid) is added into deionized water, dissolved by stirring and mixing. Adeoxidation auxiliary agent in a required amount is added to form astable solution. The stabilizer is in an amount of from 1/10 to ⅕ of thetotal weight of the deoxidation auxiliary agent. Stirring is conducteduntil complete dissolution is achieved, to obtain a stable solution.

A support is impregnated by said stable solution for from 10 min to 2 h,preferably from 0.5 to 1 h, oven-dried at 110-150° C. for 2-6 h,calcined at 200-500° C. for 2-5 h to obtain the semi-finished catalystof the present invention. The catalyst of the present inventioncomprises from 1 to 5 wt. %, preferably from 2 to 4 wt. % of FeSO₄.

3. Preparation of the Catalyst

The active component-complexing agent (citric acid or phosphoric acid)is added into deionized water and heated to more than 70° C. Cobaltsalt, molybdenum salt and nickel salt in the required amounts are addedwhile being continuously stirred, so as to form a stable solution. Thecomplexing agent is in an amount of from ⅕ to ½, preferably ⅓ of thetotal weight of the active component metal salt. Stirring is conducteduntil complete dissolution is achieved, to obtain the active componentco-impregnation solution.

A support is impregnated by said co-impregnation solution for from 10min to 3 h, preferably from 0.5 to 1 h, oven-dried at 110-150° C. for2-6 h, calcined at 200-500° C. for 2-5 h to obtain the catalyst of thepresent invention. The catalyst of the present invention comprises from0.5 to 3 wt. %, preferably from 1.0 to 1.5 wt. % of nickel oxide, from 1to 4 wt. %, preferably from 2.0 to 3.0 wt. % of cobalt oxide, from 8 to20 wt. %, preferably from 12 to 15 wt. % of molybdenum oxide, from 1 to5 wt. %, preferably from 2 to 4 wt. % of FeSO₄, from 10 to 40 wt. %,preferably from 20 to 30 wt. % of TiO₂, the balance being γ-Al₂O₃, basedon the weight percent of the catalyst.

The method for processing the sulfur-containing gas using thehydrogenation catalyst prepared according to the present inventioncomprises introducing the sulfur-containing gas into the tail gashydrogenation unit of the sulfur recovery device, processing with thehydrogenation catalyst of the present invention, absorbing thehydrogenated tail gas with a solvent and then regenerating (the same asthe original process), the regenerated hydrogen sulfide being recycledto the Claus unit to recover sulfur, the clean tail gas beingincinerated in an incinerator to reach the standards and discharged.

Wherein, (1) The hydrogenation catalyst of the present invention isprecured with the conventional Claus tail gas under the conditions of atemperature of from 220 to 280° C., a volume space velocity of from 400to 1,500 h⁻¹, from 3 to 8 vol. % of hydrogen in the feed gas; the curingis finished when the H₂S content at the outlet of the reactor is greaterthan or equal to that at the inlet of the reactor; and

-   -   (2) after curing, adjusting the inlet temperature of the        hydrogenation reactor to be from 220 to 280° C., at which the        sulfur-containing flue gas is introduced.

The sulfur-containing gas of the present invention is the gas producedduring the petrochemical processing and chemical processing of coal andcomprising one or more selected from sulfur dioxide, mercaptan,thioether, CS₂ and COS, including flue gas regenerated by absorptivedesulfurization of gasoline, flue gas regenerated by desulfurization ofliquefied gas, flue gas regenerated by catalytic cracking, Claus tailgas, boiler flue gas, preferably one or more selected from flue gasregenerated by absorptive desulfurization of gasoline, flue gasregenerated by desulfurization of liquefied gas and Claus tail gas.

Said sulfur-containing gas comprises from 0 to 6 vol. % of sulfurdioxide and 0 to 3 vol. % of oxygen and has a temperature of preferablyfrom 100 to 200° C.

Advantages of the Present Invention

The method and the catalyst of the present invention can be used forhydrogenation of the sulfur-containing gas at an inlet temperature of220-280° C., wherein said sulfur-containing gas can be processed bydirectly introducing into the tail gas processing unit of the sulfurdevice without the need of adding any other equipments. Up to now, it isthe most desirable way for processing the sulfur-containing gas, andsuch a method not only recovers the sulfur resource, but also avoids theenvironmental pollution. The hydrogenation catalyst of the presentinvention has an activity which is 30% higher than that of theconventional Claus tail gas hydrogenation catalyst, a workingtemperature which is lower by more than 60° C., a notable energy-savingand consumption reduction effect, and better economic benefits andenvironmental protection benefits.

DESCRIPTION OF THE DRAWINGS

FIG. 1 is the flow process chart of the present invention.

FIG. 2 is schematic diagram of the laboratory 10 ml sulfur micro-reactorevaluation device of the present invention.

In FIG. 1, 1—the sulfur-containing gas; 2—the hydrogen-containing Claustail gas; 3—the hydrogenation reactor; 4—the quench tower; 5—theabsorption tower; 6—the regeneration tower; 7—hydrogen sulfide isrecycled to the sulfur-producing unit; 8—the incinerator; 9—the tube forremoval of fume in the clean tail gas.

In FIG. 2, BV1-BV22—the globe valves; 3BV1-3BV2—the three way globevalves; CV1-CV6—the one way valves; EPC—the electronic pressurecontroller; F1-F8—the filters; GC—the gas chromatograph; MFC1-MFC 6—theweight flow controller; NV1-NV8—the stop valves; P—the metering pump;PIB—the standard pressure gauge; PIO1-PIO13—the pressure gauge;PRV1-PRV6—the pressure relief valves; RHC—the low temperature bath;TIC01—the temperature control; TI01—the reaction temperature display;V1—the stock tank; V2—the bubbler; V3—the drain sump; V4—the caustictreater.

EMBODIMENTS Example 1 Preparation of Titanium-Aluminum Compound DryColloid

A sodium metalluminate solution containing 40 g of Al₂O₃/L was placed ina colloid-forming tank, and the colloid-forming temperature wascontrolled to be 20° C. CO₂ having a volume concentration of 35% was fedfor neutralization, and metatitanic acid was pulped. When CO₂ began tobe fed, metatitanic acid slurry was slowly added for a period of timewhich was controlled to be 10-20 min, so as to make the weight contentof titania achieve 50% in the dry colloid, and to control the pH valueof the glue solution to be 10-12. After stopping the colloidization, atitanium-aluminum compound dry colloid 1 was prepared by filtering,washing, drying and pulverizing to 180 meshes. By the same method, atitanium-aluminum compound dry colloid 2 having a titania content of40%, a titanium-aluminum compound dry colloid 3 having a titania contentof 30%, a titanium-aluminum compound dry colloid 4 having a titaniacontent of 20%, a titanium-aluminum compound dry colloid 5 having atitania content of 10%, and a titanium-aluminum compound dry colloid 6having a titania content of 0% were also prepared. The physicochemicalproperties of dry colloids having different titania contents are shownin Table 1.

TABLE 1 Physicochemical properties of dry colloids having different TiO₂contents Dry Pore volume/ Specific surface colloid TiO₂, % ml · g⁻¹area/m² · g⁻¹ 1 50 0.52 249 2 40 0.60 281 3 30 0.71 313 4 20 0.80 345 510 0.89 379 6 0 0.98 410

Example 2 Preparation of Titanium-Aluminum Compound Dry Colloid Support

100 g of titanium-aluminum compound dry colloids with different TiO₂contents were respectively weighed and added into a kneader. 5 g ofsesbania powder was also added and homogeneously stirred. 4 g of nitricacid (65%, m/m) was dissolved in 80 ml of deionized water to formulate anitric acid solution. The nitric acid solution was added into thekneader. The mixture was kneaded to become lumpy, molded by extrusion ona bar-extruder with φ3 mm clover-type or four-leaf clover-type poreplate, dried at 110° C. for 4 h, calcined at 550° C. for 4 h to produceTiO₂—Al₂O₃ compound support series. The properties thereof are shown inTable 2.

TABLE 2 Physicochemical properties of the support Pore volume/ Specificsurface Support TiO₂, % ml · g⁻¹ area/m² · g⁻¹ 1 50 0.26 209 2 40 0.33238 3 30 0.45 270 4 20 0.55 318 5 10 0.62 353 6 0 0.71 368

Example 3 Preparation of the Semi-Finished Product of the Catalyst

70 g of deionized water and 3 g of citric acid were added into areaction bottle, stirred and mixed. Then 50 g of ferrous sulfate wasadded therein, dissolved by stirring until the solution was transparent,to formulate a stable impregnation solution. 10 g of No. 1-6 supports inTable 1 were respectively impregnated for 1 h while maintaining the sameferrous sulfate content, oven-dried at 110° C. for 4 h, calcined at 400°C. for 4 h to produce the semi-finished products 1-1, 2-1, 3-1, 4-1, 5-1and 6-1. The properties thereof are shown in Table 3.

TABLE 3 Physicochemical properties of the semi- finished products of thecatalyst Properties 1-1 2-1 3-1 4-1 5-1 6-1 Specific 192 213 248 301 335346 surface area/m² · g⁻¹ Pore volume/ 0.25 0.31 0.42 0.50 0.56 0.64 ml· g⁻¹ Crushing 192 198 195 188 186 188 strength/ N · cm⁻¹ FeSO₄ weight 55 5 5 5 5 percent, %

Example 4 Preparation of the Catalyst Series 1-2, 2-2, 3-2, 4-2, 5-2 and6-2

100 g of deionized water and 18 g of phosphoric acid were added into areaction tank and heated. Then 54 g of ammonium molybdate and 11 g ofbasic cobalt carbonate were dissolved therein, dissolved by stirringuntil the solution was transparent. 9 g of nickel carbonate was added,dissolved by stirring until the solution was transparent, to formulate apurple, transparent cobalt, molybdenum and nickel impregnation solution.According to the water absorption of the semi-finished catalyst productsin Table 2, 10 g of the semi-finished products 1-1, 2-1, 3-1, 4-1, 5-1and 6-1 were respectively impregnated for 1 h, oven-dried at 110° C. for4 h, calcined at 400° C. for 4 h to produce the catalyst series 1-2,2-2, 3-2, 4-2, 5-2 and 6-2. The properties thereof are shown in Table 4.

TABLE 4 Physicochemical properties of the catalyst Properties 1-2 2-23-2 4-2 5-2 6-2 Specific 160 178 222 259 281 312 surface area/m² · g⁻¹Pore volume/ 0.28 0.31 0.41 0.47 0.51 0.54 m² · g⁻¹ Crushing 190 192 190183 185 182 strength/ N · cm⁻¹ Bulk density/ 0.85 0.80 0.75 0.70 0.640.62 kg · L⁻¹ TiO₂ weight 37.5 30.0 22.5 15.0 7.5 0 percent, % FeSO₄weight 4 4 4 4 4 4 percent, % MoO₃ weight 15 15 15 15 15 15 percent, %(CoO + NiO) 3.5 3.5 3.5 3.5 3.5 3.5 weight percent, %

Example 5 Evaluation of the Catalyst Activity

Evaluation of the catalyst activity was conducted in a 10 mlmicro-reactor. The reactor was made of stainless steel tube having aninner diameter of 20 mm, placed in a thermostat which was electricallyheated, similar to an equi-heat furnace. The catalyst has a loadingamount of 10 mL with a particle size of 20-40 meshes. Quartz sand havingthe same particle size was loaded onto the upper of the catalyst, mixedand pre-heated. SHIMUZU GC-2014 gas chromatograph was used to on-lineanalyze the content of H₂S, SO₂ and CS₂ in the gas at the inlet andoutlet of the reactor; the chromatographic column loaded with GDX-301carrier was used to analyze the sulfide, wherein the column temperaturewas 120° C.; a thermal conductivity detector was used; hydrogen was usedas the carrier gas; the post-column flow rate was 28 mL/min.

The technological process of the laboratory micro-reactor evaluationdevice is shown in FIG. 2.

The gas composition of Claus tail gas and flue gas regenerated byabsorptive desulfurization of gasoline was simulated, controlled bycontrolling the flow rate of N₂, air, CO₂, H₂S, SO₂, CS₂, O₂, H₂ andwater vapor, pre-heated to a certain temperature (200-260° C.) and thenfed into a fixed bed reactor loaded with catalysts and fillers. Afterthe gas was hydrogenated, and the sulfur-containing compound wasabsorbed by an alkaline solution (10% sodium hydroxide), the clean tailgas was discharged into air. Tests of analyzing the composition of agroup of feed gas and tail gas per hour were conducted, and the resultsare used as the basis for calculating the activities of the catalysts.

After the testing equipment passed the airtightness testing, thecatalyst was precured by the conventional dry process at a normalpressure, a volume space velocity of 1250 h⁻¹, wherein the sulfurizationgas was hydrogen plus 2(v) % of hydrogen sulfide.

Sulfurization steps: heating with nitrogen gas to 200° C. in a rate of50° C./h by adjusting the nitrogen gas flow according to the spacevelocity, switching to sulfurization gas and adjusting the gas flow,continuing to heat to 240° C., maintaining the temperature for 3 h,finishing the sulfurization after hydrogen sulfide at the outlet andinlet of the reactor reached an equilibrium, then switching to thereaction gas comprising 1.2 vol. % of SO₂, 10 vol. % of H₂, 0.4 vol. %of O₂, 0.5 vol. % of CS₂, 30 vol. % of H₂O, and the balance beingnitrogen gas. The SO₂ hydrogenation activity of the catalysts wasevaluated by using 3H₂+SO₂→H₂S+2H₂O as the indicator reaction; theorganic sulfur hydrolysis activity of the catalysts was evaluated byusing CS₂+H₂O→CO₂+H₂S as the indicator reaction; the O₂ removal activityof the catalysts was evaluated by using 2H₂+O₂→2H₂O as the indicatorreaction. The gas volume space velocity was 1250 h⁻¹, and the reactiontemperature was 240° C. The hydrogenation conversion activity of thecatalysts was calculated according to the following formula:

$\eta_{{SO}\; 2\mspace{14mu}{or}\mspace{14mu}{CS}\; 2\mspace{14mu}{or}\mspace{14mu} O\; 2} = {\frac{M_{0} - M_{1}}{M_{0}} \times 100\%}$wherein M₀ and M₁ respectively represent the volume concentrations ofSO₂, O₂ or CS₂ at the inlets and outlets of the reactor.

The SO₂ hydrogenation and CS₂ hydrolysis activities of the catalysts inTable 4 are shown in Table 5.

TABLE 5 Activities of the hydrogenation catalysts Items 1-2 2-2 3-2 4-25-2 6-2 SO₂ hydrogenation 93.2 96.8 100 100 96.5 93.9 conversion rate, %CS₂ hydrolysis rate, % 90.6 98.2 100 100 93.5 88.1 O₂ hydrogenation 100100 100 100 100 100 conversion rate, %

Example 6 Preparation of the Catalyst Series Having Different MetalContents

No. 3 support prepared according to Example 2 was used to produce asemi-finished product according to Example 3, and then to furtherproduce the catalysts 3-2, 3-3, 3-4, 3-5 and 3-6 having different metalcontents according to Example 4. The physicochemical properties thereofare shown in Table 6.

TABLE 6 Physicochemical properties of the catalysts Properties 3-2 3-33-4 3-5 3-6 Specific surface 245 238 230 222 209 area/m² · g⁻¹ Porevolume/m² · g⁻¹ 0.43 0.42 0.42 0.41 0.40 Crushing strength/ 190 185 188190 189 N · cm⁻¹ Bulk density/kg · L⁻¹ 0.73 0.74 0.74 0.75 0.76 FeSO₄weight percent, % 5.0 2.0 4.0 4.0 1.0 MoO₃ weight percent, % 10.0 12.012.0 15.0 20.0 (CoO + NiO) weight 2.5 3.0 3.0 3.5 5.0 percent, %

According to the method for activity evaluation of the catalysts inExample 5, the activity evaluation was conducted for 5 catalysts inTable 6, and the SO₂ hydrogenation and CS₂ hydrolysis activities areshown in Table 7.

TABLE 7 Activities of the hydrogenation catalysts Items 3-2 3-3 3-4 3-53-6 SO₂ hydrogenation 100 100 100 100 100 conversion, % CS₂ hydrolysisrate, % 100 100 100 100 100 O₂ hydrogenation 100 100 100 100 100conversion rate, %

Example 7 Comparison Example

According to the method for preparation of the catalyst in Example 4,No. 3 support prepared according to Example 2 was made without theprocedure of the preparation of the semi-finished product in Example 3into a hydrogenation catalysts 3-7 containing no deoxidation auxiliaryagent. The comparison of the physicochemical properties of the catalystand the catalyst of the present invention are shown in Table 8.

TABLE 8 Comparison of the physicochemical properties of the catalystsCatalyst of the Properties Catalyst 3-7 present invention Activecomponent content: MoO₃, weight % 15.0 15.0 (CoO + NiO) weight % 3.5 3.5FeSO₄ weight % 0 4.0 Side pressure strength/N · cm⁻¹ 295 305 Specificsurface area/m² · g⁻¹ 195 189 Pore volume/ml · g⁻¹ 0.32 0.32 Bulkdensity/kg · L⁻¹ 0.79 0.80

According to the method for activity evaluation of the catalyst inExample 5, the comparison between the hydrogenation activities of thecatalyst 3-7 and the catalyst of the present invention is shown in Table9.

TABLE 9 Comparison of the activities of the catalysts Catalysts Catalystof the Temperature/° C. Items 3-7 present invention 220 SO₂hydrogenation 90 96 conversion, % CS₂ hydrolysis rate, % 82 91 O₂removal rate, % 30 90 240 SO₂ hydrogenation 98 100 conversion, % CS₂hydrolysis rate, % 95 100 O₂ removal rate, % 50 98

Table 9 shows that the addition of deoxidation auxiliary agent greatlyincreases the deoxidation activity of the catalyst of the presentinvention, and increases the low temperature SO₂ hydrogenation andorganic sulfur hydrolysis activities of the catalyst, which shows thatthe deoxidation auxiliary agent and the active components have bettersynergistic effect therebetween.

Example 8 Physicochemical Property Comparison between the ConventionalClaus Tail Gas Hydrogenation Catalyst and the Catalyst of the PresentInvention

Physicochemical property comparison between the conventional Claus tailgas hydrogenation catalyst and the catalyst of the present invention isshown in Table 10.

TABLE 10 Comparison of the physicochemical properties of the catalystsConventional Claus tail gas hydrogenation Catalyst of the presentProperties catalyst invention Active component content: MoO₃ weight %10.0 15.0 (CoO + NiO) weight % 2.5 3.5 FeSO₄ weight % 0 4.0 Sidepressure strength/N · cm⁻¹ 165 305 Specific surface area/m² · g⁻¹ 320189 Pore volume/ml · g⁻¹ 0.50 0.32 Bulk density/kg · L⁻¹ 0.60 0.80Support Alumina Titanium-aluminum compound support

According to the method for activity evaluation of the catalyst inExample 5, the comparison between the activities of the conventionalClaus tail gas hydrogenation catalyst and the catalyst of the presentinvention is shown in Table 11.

TABLE 11 Comparison of the catalyst activities Conventional CatalystClaus tail gas of the hydrogenation present Temperature/° C. Itemscatalyst invention 240 SO₂ hydrogenation 76 100 conversion, % CS₂hydrolysis rate, % 68 100 O₂ removal rate, % 45 98 260 SO₂ hydrogenation95 100 conversion, % CS₂ hydrolysis rate, % 98 100 O₂ removal rate, % 92100 280 SO₂ hydrogenation 100 100 conversion, % CS₂ hydrolysis rate, %100 100 O₂ removal rate, % 100 100

Table 11 shows that the catalyst of the present invention has betterlow-temperature SO₂ hydrogenation activity, organic sulfur hydrolysisactivity and deoxidation activity, while the conventional Claus tail gashydrogenation catalyst cannot satisfy the requirements on the SO₂hydrogenation, organic sulfur hydrolysis and deoxidation unless there isa higher reaction temperature. Moreover, when the sulfur-containing gashas a higher SO₂ content, the conventional Claus tail gas hydrogenationcatalyst is easy to sulfatize, so that SO₂ penetrate the catalyst bedlayer.

Example 9 Industrial Application Tests of the Catalyst

The catalyst 3-2 of the present invention was prepared and loaded intothe tail gas hydrogenation reactor of the industrial sulfur device. Theprocess chart for treating the regenerated flue gas is shown in FIG. 1.

The catalyst 3-2 was precured by the conventional Claus tail gas at atemperature of 220-280° C., a volume space velocity of 400-1,500 h⁻¹,wherein hydrogen was in an amount of 3-8 vol. % of the feed gas. WhenH₂S content at the outlet of the reactor was greater than or equal tothat at the inlet thereof, sulfurization stopped. After sulfurization,the temperature at the inlet of the hydrogenation reactor was adjustedto 220-280° C. While introducing the Claus tail gas, flue gasregenerated by absorptive desulfurization of gasoline was alsointroduced. The composition, flow rate and temperature of the flue gasregenerated by absorptive desulfurization of gasoline are shown in Table12.

TABLE 12 Composition, flow rate and temperature of the regenerated fluegas Temperature Flow rate/ when entering the No. Nm³ · h⁻¹ SO₂ vol. % O₂vol. % reactor/° C. 1 329 2.91 0.00 131 2 423 0.16 2.60 133 3 554 3.320.05 129 4 764 1.76 0.86 125 5 611 1.58 0.98 132 6 636 0.51 1.25 132 7506 2.40 0.30 128 8 371 0.17 1.20 129 9 256 1.96 0.03 126 10 261 0.093.42 133 11 95 3.16 0.00 133

According to the data in Table 12, it can be seen that the flow rate ofthe flue gas regenerated by absorptive desulfurization of gasoline has agreat fluctuation; the SO₂ content in the flue gas regenerated byabsorptive desulfurization of gasoline has a great fluctuation with themaximum of 3.32% and the minimum of 0.09%; the oxygen content in theflue gas regenerated by absorptive desulfurization of gasoline has agreat fluctuation with the maximum of 3.42% and the minimum of 0.00%;the flue gas regenerated by absorptive desulfurization of gasolineentering the reactor has a lower temperature, wherein the temperature isjust 126-133° C. in summer and will be much lower in winter.

Example 10 Effect on the Temperature Rise of the Catalyst Bed Layerbefore and after Introducing the Flue Gas Regenerated by AbsorptiveDesulfurization of Gasoline

The normal temperature rise of the bed layer for the Claus tail gashydrogenation was 30-40° C. After the introduction of the flue gasregenerated by absorptive desulfurization of gasoline, the flow rate ofthe Claus tail gas was 2,000-3,000 Nm³/h; the flow rate of the flue gasregenerated by absorptive desulfurization of gasoline was about300-1,000 Nm³/h, wherein the flow rate of the flue gas regenerated byabsorptive desulfurization of gasoline was 30% of the normal flow rateof the Claus tail gas. The effects on the catalyst bed layer before andafter the introduction of the regenerated flue gas are shown in Table13.

TABLE 13 Change of the temperature rise of the catalyst bed layer beforeand after introducing the flue gas regenerated by absorptivedesulfurization of gasoline temperature Inlet/ upper/ middle/ bottom/rise of the bed Materials ° C. ° C. ° C. ° C. layer/° C. Claus tail gas234 244 256 266 32 243 266 277 280 37 247 272 282 285 38 Claus tailgas + 256 283 291 291 35 Flue gas by 248 295 310 314 66 absorptive 247296 311 312 65 desulfurization of 246 304 323 325 79 gasoline 244 305321 321 77 247 300 317 320 73 247 297 312 315 68 247 297 317 319 72 244283 295 297 53 243 294 308 314 71 244 283 297 299 55 246 296 309 311 65

According to the results in Table 13, it can be seen that the normal bedlayer temperature rise of the Claus tail gas hydrogenation is 30-40° C.,and is increased to 50-80° C. after the introduction of the flue gasregenerated by absorptive desulfurization of gasoline. Since thecatalyst of the present invention has a better low-temperaturehydrogenation activity, the inlet temperature of the hydrogenationreactor was controlled to be 240-250° C., and the maximum temperature ofthe bed layer may be 325° C., while the normal application temperatureof the catalyst of the present invention is 220-360° C. Due to unstableflow rate and composition of the flue gas regenerated by absorptivedesulfurization of gasoline, the temperature rise of the bed layer maybe varied, but without overtemperature or huge fluctuation of the bedlayer, which shows that the catalyst of the present invention cansatisfy the requirements on the flow rate and composition fluctuation ofthe flue gas regenerated by absorptive desulfurization of gasoline.

Example 11 Composition of the Gas at the Outlet of the HydrogenationReactor after Introducing the Flue Gas Regenerated by AbsorptiveDesulfurization of Gasoline

The composition of the gas at the outlet of the hydrogenation reactorafter introducing the flue gas regenerated by absorptive desulfurizationof gasoline is shown in Table 14.

TABLE 14 Composition of the gas at the outlet of the hydrogenationreactor No. H₂S vol. % SO₂ vol. % O₂ vol. % 1 2.41 0 0 2 2.16 0 0 3 1.860 0 4 1.52 0 0 5 2.15 0 0 6 1.54 0 0 7 2.41 0 0 8 2.92 0 0 9 2.30 0 0 100.62 0 0 11 2.23 0 0

According to the data in Table 14, it can be seen that the presence ofSO₂ or O₂ is not detected in the hydrogenated tail gas, which shows thatthe catalyst of the present invention has a better hydrogenation effect.Under the circumstance that SO₂ is in a higher content in the processgas, and in the presence of oxygen, the catalyst of the presentinvention can satisfy the requirements on the flow rate and compositionfluctuation of the flue gas regenerated by absorptive desulfurization ofgasoline.

The invention claimed is:
 1. A hydrogenation catalyst, characterized inthat the catalyst comprises from 0.5 to 3 wt. % of an active componentnickel oxide; from 1 to 4 wt. % of an active component cobalt oxide;from 8 to 20 wt. % of an active component molybdenum oxide or tungstenoxide; from 1 to 5 wt. % of a deoxidation auxiliary agent selected fromone or more of ferrous sulfate, ferric nitrate and ferric sulfate; from10 to 40 wt. % of TiO₂, the balance being γ-Al₂O₃, based on the weightof the catalyst, wherein TiO₂ and γ-Al₂O₃ are added in the form oftitanium-aluminum compound dry colloid.
 2. The hydrogenation catalystaccording to claim 1, characterized in that the deoxidation auxiliaryagent is ferrous sulfate.
 3. The hydrogenation catalyst according toclaim 1, characterized in that the catalyst comprises from 1.0 to 1.5wt. % of an active component nickel oxide, from 2.0 to 3.0 wt. % of anactive component cobalt oxide, from 12 to 15 wt. % of an activecomponent molybdenum oxide or tungsten oxide, from 2 to 4 wt. % of adeoxidation auxiliary agent, from 20 to 30 wt. % of TiO₂, the balancebeing γ-Al₂O₃, based on the weight of the catalyst.
 4. The hydrogenationcatalyst according to claim 1, which is produced by the following steps:using titanium-aluminum compound dry colloid as the main material,bar-extruding, drying, calcining to prepare a support; said supportbeing impregnated with a deoxidation auxiliary agent, dried, calcined toproduce a semi-finished product; said semi-finished product beingimpregnated with an impregnation solution of the active componentsnickel, cobalt and molybdenum compounds, further dried and calcined. 5.The hydrogenation catalyst according to claim 4, characterized in thatsaid titanium-aluminum compound dry colloid is produced by feeding CO₂having a volume concentration of 3-40% into a sodium metalluminatesolution of 5-60 g of Al₂O₃/L for neutralization, adding metatitanicacid slurry simultaneously, so as to make the weight content of titaniaachieve 30-60% in the dry colloid, controlling the pH value of the gluesolution to be 10-12, stopping the colloidization, filtering, washing,drying and pulverizing to produce a titanium-aluminum compound drycolloid.
 6. The hydrogenation catalyst according to claim 5,characterized in that the titanium-aluminum compound dry colloid has apore volume of greater than 0.6 ml/g, a specific surface area of greaterthan 250 m²/g, a sodium weight content of less than 0.1%, and a SO₄ ²⁻weight content of less than 0.2%.
 7. The hydrogenation catalystaccording to claim 6, characterized in that the titanium-aluminumcompound dry colloid has a pore volume of from 0.60 to 0.90 mL/g and aspecific surface area of from 270 to 380 m²/g.
 8. A method forprocessing a sulfur-containing gas with the hydrogenation catalystaccording to claim 1, characterized in introducing the sulfur-containinggas into the tail gas hydrogenation unit of a sulfur recovery device,processing it with said hydrogenation catalyst, absorbing thehydrogenated tail gas with a solvent and then regenerating, theregenerated hydrogen sulfide being recycled to the Claus unit to recoversulfur, the clean tail gas being incinerated in an incinerator to bedischarged after reaching the standards.
 9. The method for processing asulfur-containing gas according to claim 8, characterized in that thesulfur-containing gas is one or more selected from flue gas regeneratedby adsorptive desulfurization of gasoline, flue gas regenerated bydesulfurization of liquefied gas and Claus tail gas.
 10. The method forprocessing a sulfur-containing gas according to claim 8, characterizedin that (1) the hydrogenation catalyst is precured with Claus tail gasunder the conditions of a temperature of from 220 to 280° C., a volumespace velocity of from 400 to 1,500 h⁻¹, from 3 to 8 vol. % of hydrogenin the feed gas, the curing is finished when the H₂S content at theoutlet of the reactor is greater than or equal to that at the inlet ofthe reactor; and (2) after curing, adjusting the inlet temperature ofthe hydrogenation reactor to be from 220 to 280° C., at which thesulfur-containing gas is introduced.
 11. The method for processing asulfur-containing gas according to claim 8, characterized in that thesulfur-containing gas comprises from 0 to 6 vol. % of sulfur dioxide andfrom 0 to 3 vol. % of oxygen.
 12. The method for processing asulfur-containing gas according to claim 8, characterized in that thesulfur-containing gas enters the sulfur device at a temperature of from100 to 200° C.